CN202122945U - Circulating fluidized bed type low-carbon alkane dehydrogenizing and olefin generating device - Google Patents
Circulating fluidized bed type low-carbon alkane dehydrogenizing and olefin generating device Download PDFInfo
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- CN202122945U CN202122945U CN2011201481195U CN201120148119U CN202122945U CN 202122945 U CN202122945 U CN 202122945U CN 2011201481195 U CN2011201481195 U CN 2011201481195U CN 201120148119 U CN201120148119 U CN 201120148119U CN 202122945 U CN202122945 U CN 202122945U
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- regenerator
- reactor
- fluidized bed
- reduction
- catalyst
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- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 29
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 25
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims description 16
- 239000003054 catalyst Substances 0.000 claims abstract description 49
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 24
- 239000011651 chromium Substances 0.000 claims description 12
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 11
- 229910052804 chromium Inorganic materials 0.000 claims description 11
- 150000001335 aliphatic alkanes Chemical class 0.000 claims 3
- 230000008929 regeneration Effects 0.000 abstract description 27
- 238000011069 regeneration method Methods 0.000 abstract description 27
- 238000006243 chemical reaction Methods 0.000 abstract description 20
- 238000000034 method Methods 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 5
- 239000000571 coke Substances 0.000 description 20
- 238000004519 manufacturing process Methods 0.000 description 11
- 230000001172 regenerating effect Effects 0.000 description 11
- 230000003134 recirculating effect Effects 0.000 description 9
- 239000007789 gas Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 239000012752 auxiliary agent Substances 0.000 description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 4
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 description 3
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 3
- 229910000423 chromium oxide Inorganic materials 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
- 239000001282 iso-butane Substances 0.000 description 2
- 235000013847 iso-butane Nutrition 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 229910052718 tin Inorganic materials 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
本实用新型涉及循环流化床低碳烷烃脱氢制烯烃装置，采用流化床型反应再生系统，在催化剂的存在下，利用低碳烷烃制取烯烃，该装置包括反应器、再生器、还原汽提器及管线，反应器、再生器、还原汽提器为独立的设备，反应器与再生器设在两侧，通过管线连接，还原汽提器设在反应器与再生器的中间，经管线与再生器和反应器分别连接。与现有技术相比，本实用新型具有还原再生设备独立，还原再生过程不受烧焦再生过程的制约，还原效果理想，操作安全等优点。
The utility model relates to a device for producing olefins by dehydrogenating low-carbon alkanes in a circulating fluidized bed. A fluidized bed type reaction regeneration system is used to produce olefins by using low-carbon alkanes in the presence of a catalyst. The device includes a reactor, a regenerator, a reducing The stripper and pipeline, the reactor, the regenerator, and the reduction stripper are independent equipment. The reactor and the regenerator are arranged on both sides and connected by pipelines. The reduction stripper is arranged in the middle of the reactor and the regenerator. Pipelines are connected to the regenerator and reactor respectively. Compared with the prior art, the utility model has the advantages of independent reduction and regeneration equipment, the reduction and regeneration process is not restricted by the burnt regeneration process, the reduction effect is ideal, and the operation is safe.
Description
Technical field
The utility model relates to a kind of manufacturing olefin by low-carbon alkane dehydrogenation device, especially relates to a kind of recirculating fluidized bed manufacturing olefin by low-carbon alkane dehydrogenation device.
Background technology
Because the shortage of alkene resource, the technology of manufacturing olefin by low-carbon alkane dehydrogenation come into one's own gradually and develop rapidly.Known manufacturing olefin by low-carbon alkane dehydrogenation technology has catalytic oxidative dehydrogenation technology, fixed-bed catalytic dehydrogenating technology, moving bed catalytic dehydrogenation process and circulating fluid bed catalysis dehydrogenating technology.Wherein, the recirculating fluidized bed dehydrogenating technology is high because of its heat transfer efficiency, and conversion ratio is stable, and advantages such as handling safety become the main mode that dehydrogenating low-carbon alkane is produced alkene gradually.
The characteristic of recirculating fluidized bed manufacturing olefin by low-carbon alkane dehydrogenation technology is to adopt fluidized-bed reactor and regenerator.Catalyst circulates between reactor and regenerator with fluidized.Dehydrogenation reaction takes place in reactor; In regenerator, make catalyst regeneration through the coke that during reaction is deposited on the catalyst of burning, add postcombustion simultaneously keeping bed temperature, the circulation through catalyst is the reaction system heat supply.
CN1213662A discloses a kind of method that obtains light olefin through dehydrogenation of corresponding paraffins in 1999; The process for dehydrogenating light paraffins that CN1082018A disclosed in a kind of fluidized-bed reactor in 1994; CN201140065Y discloses a kind of riser recirculating fluidized bed dehydrogenating low-carbon alkane olefin hydrocarbon apparatus in 2008, all these belongs to the research and the application of recirculating fluidized bed manufacturing olefin by low-carbon alkane dehydrogenation technology.
At present, be applied to the dehydrogenating low-carbon alkane catalyst for reaction and be mainly chromium-based catalysts and platinum group catalyst.The composition of chromium-based catalysts generally comprises chromium oxide, alkali metal oxide, alumina carrier and other auxiliary agents.Chromium is active component wherein.Point out in " Cr is the propane dehydrogenation catalyst progress " that Tan Xiaolin etc. once published in 2010 the 29th the 1st phases of volume of chemical industry progress periodical: the existing way of chromium has Cr6+, Cr5+, Cr3+ etc. in the chromium-based catalysts; The chromium of various prices has different catalysis behavior and selectivity, and wherein Cr3+ has determined the catalytic activity and the propylene selectivity of catalyst.The Application Research of platinum group catalyst wants Zao than chromium-based catalysts, and its composition generally comprises platinum, tin, alumina carrier and other auxiliary agents, owing to it costs an arm and a leg, so generally be used for fixing a reaction system.
The particularity of low-carbon alkanes catalytic dehydrogenating reaction technology is: its catalyst system and catalyzing constantly circulates in reduction atmosphere and oxidation atmosphere; When carrying out dehydrogenation reaction, catalyst is in the reduction atmosphere, and active component is reduced, and is in lower valency, has high catalytic activity and reaction selectivity; When carrying out coke burning regeneration, catalyst is in the oxidation atmosphere, and active component is all or part of oxidized, becomes high valence state, and reactivity and selectivity reduce.
Catalyst behind coke burning regeneration is not treated; When directly the entering reactor contacts with paraffinic feedstock, since active low with selectivity, cause conversion ratio side reaction low and that do not expect to take place; Formation has the accessory substance and the coking of relative broad range carbon number; Make follow-up product separate and become complicated, the productive rate of alkene descends, and system operation cost increases.Regenerator in the technology that has (CN1213662A) contains reduction section, fuses with regenerator; But the consumption of the feasible kind as the catalyst reduction agent of such layout, reducing agent, the temperature of reduction, pressure condition etc. all receive the restriction of the safety of regenerator, the temperature of coke burning regeneration etc., and reduction effect is undesirable.
Summary of the invention
The purpose of the utility model is exactly the restriction of the coke burning regeneration conditions such as temperature of the safety that provides a kind of reduction process not receive regenerator in order to overcome the defective that above-mentioned prior art exists, coke burning regeneration; Reducing/regenerating is satisfactory for result, the recirculating fluidized bed manufacturing olefin by low-carbon alkane dehydrogenation device that activity of such catalysts and selectivity are high.
The purpose of the utility model can realize through following technical scheme:
A kind of recirculating fluidized bed manufacturing olefin by low-carbon alkane dehydrogenation device, this device adopts the fluidized-bed reaction regenerative system, in the presence of catalyst, prepares corresponding alkene by dehydrogenating low-carbon alkane.It is characterized in that: this device comprises reactor, regenerator, reduction stripper and pipeline; Reactor, regenerator and reduction stripper are three separate equipment; Described reactor and described regenerator are located at both sides; Connect through pipeline, described reduction stripper be located at reactor and with the centre of regenerator, be connected respectively with reactor with regenerator through pipeline.
Dehydrogenation reaction takes place in catalyst and low-carbon alkanes in reactor; The catalyst of inactivation gets into regenerator from reactor and carries out coke burning regeneration; Catalyst behind the coke burning regeneration gets into the reduction stripper from regenerator and carries out reducing/regenerating; Catalyst circulation behind the reducing/regenerating gets into reactor, participates in reaction again.
Described catalyst is preferably chromium-based catalysts.
The composition of described chromium-based catalysts comprises chromium oxide, alkali metal oxide, alumina carrier and other auxiliary agent.
Described low-carbon alkanes comprises that arbitrary component or said components among ethane, propane, normal butane, iso-butane, pentane, isopentane or the C6-C8 is with the mixture of various compositions of proportions.
Described coke burning regeneration is in the presence of air or oxygen and another kind of postcombustion, burns the coke that catalyst surface gathers, and controls and burn temperature through regulating postcombustion.
The required heat of described dehydrogenation reaction is provided by the coke burning regeneration section, brings reactor into through catalyst circulation.
Described reducing/regenerating is in the presence of reducing gases, carrier gas and regeneration gas, reduction oxidized activity of such catalysts component in coke burning regeneration.
Described reactor is a fluid bed-type of reactor.
Described regenerator is the fluidized bed type regenerator.
Described reduction stripper is a fluidized bed type reduction stripper.
Reaction temperature in the described reactor is 450-700 ℃.
Reaction temperature in the described regenerator is 600-750 ℃.
Compared with prior art, the catalyst regeneration process of the utility model is used two separate equipment: regenerator and reduction stripper.In regenerator, carry out coke burning regeneration, burn the catalyst surface coke and obtain the required heat of reaction.Carry out reducing/regenerating in reduction in the stripper, the reduction coke burning regeneration in the stage because oxidation loses activity and active component optionally, the temperature of further regulating activity of such catalysts, selectivity and catalyst.Coke burning regeneration and reducing/regenerating independently carry out, and the kind of reducing agent, consumption and restoring operation condition do not receive the coke burning regeneration process to limit flexible operation.The reactivity of the catalyst of regeneration and selectivity can reduce the generation of side reaction thus all than the height of prior art in this way, increase the conversion ratio of reactant and the productive rate of target product, reduce the load of operating cost and later separation operation.
Description of drawings
Fig. 1 is the structural representation of the utility model.
The specific embodiment
Embodiment
A kind of recirculating fluidized bed manufacturing olefin by low-carbon alkane dehydrogenation device; Its structure is as shown in Figure 1, adopts the fluidized-bed reaction regenerative system, in the presence of catalyst; Utilize low-carbon alkanes to produce alkene, this device comprises regenerator 1, reactor 2, reduction stripper 3 and connecting line.Regenerator 1, reactor 2, reduction stripper 3 are separate equipment; Reactor 2 is located at both sides with regenerator 3; Connect through first pipeline 4, reduction stripper 3 be located at reactor 2 and with the centre of regenerator 1, be connected with reactor 2 with regenerator 1 respectively with the 3rd pipeline 6 through second pipeline 5.Regenerator 1, reactor 2, reduction stripper 3 are the fluidized bed type structure.
The utility model in use; Dehydrogenation reaction takes place in catalyst and low-carbon alkanes in reactor 2; The catalyst of inactivation gets into regenerator 1 from reactor 2 and carries out coke burning regeneration; Catalyst behind the coke burning regeneration gets into reduction stripper 3 from regenerator 1 and carries out reducing/regenerating, and the catalyst circulation behind the reducing/regenerating gets into reactor 2, participates in reaction again.Reaction temperature in the regenerator 1 is 600-750 ℃, and the reaction temperature in the reactor 2 is 450-700 ℃.Use therein catalyst is preferably chromium-based catalysts, forms to comprise chromium oxide, alkali metal oxide, alumina carrier and other auxiliary agent.Low-carbon alkanes comprises that arbitrary component or said components among ethane, propane, normal butane, iso-butane, pentane, isopentane or the C6-C8 is with the mixture of various compositions of proportions.Shown in specific as follows:
Low-carbon alkanes 7 gets into reactor 2 through distributor, and product is left reactor 2 through forming logistics 8 after the proper process.The catalyst that regeneration is good gets into reactor 2 through the 3rd pipeline 6 autoreduction strippers 3, contacts with low-carbon alkanes 7 and reacts.Reacted reclaimable catalyst gets in the regenerator 1 through first pipeline 4 after stripping is handled, and carries out coke burning regeneration.Combustion-supporting gas 9 gets into regenerator 1 with postcombustion 10 through distributor.Burn tail gas and leave regenerator 2 through forming logistics 11 after the proper process.Regenerated catalyst gets in the reduction stripper 3 through second pipeline 5 and carries out reducing/regenerating.Reducing gases 13, stripping gas 12 and carrier gas 15 get into reduction stripper 3 through distributor.Reduction, stripping tail gas leave reduction stripper 3, the unit that the supply that acts as a fuel needs through forming logistics 14 after the proper process.Catalyst behind reduction, the stripping gets into reactor 2 through the 3rd pipeline 6.
Utilize manufacturing olefin by low-carbon alkane dehydrogenation in this way, the reactivity and the selectivity of regeneration rear catalyst are high, and side reaction is few, has increased the conversion ratio of reactant and the productive rate of target product, has reduced the load of operating cost and later separation operation.
Claims (5)
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011201481195U CN202122945U (en) | 2011-05-11 | 2011-05-11 | Circulating fluidized bed type low-carbon alkane dehydrogenizing and olefin generating device |
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| CN2011201481195U CN202122945U (en) | 2011-05-11 | 2011-05-11 | Circulating fluidized bed type low-carbon alkane dehydrogenizing and olefin generating device |
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| CN202122945U true CN202122945U (en) | 2012-01-25 |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013177723A1 (en) * | 2012-06-01 | 2013-12-05 | 中国石油天然气集团公司 | Process for producing olefin by dehydrogenation of alkane |
| CN104069778A (en) * | 2013-03-27 | 2014-10-01 | 中国石油天然气集团公司 | On-line sulfuration fluidized bed reaction device for olefin production by alkane dehydrogenation and method |
| CN104069779B (en) * | 2013-03-27 | 2016-08-31 | 中国石油天然气集团公司 | The fluidized bed reaction of a kind of dehydrating alkanes alkene and method |
| CN108654526A (en) * | 2017-04-01 | 2018-10-16 | 中国石油大学(华东) | A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing |
| CN111632573A (en) * | 2015-06-26 | 2020-09-08 | 陶氏环球技术有限责任公司 | Fluid solid contacting device |
| CN112569872A (en) * | 2020-11-24 | 2021-03-30 | 西南化工研究设计院有限公司 | Moving bed system for preparing low-carbon olefin by dehydrogenating low-carbon alkane |
| CN109603690B (en) * | 2019-01-08 | 2021-10-22 | 上海河图工程股份有限公司 | A reforming reactor and its application |
| CN115350652A (en) * | 2022-08-04 | 2022-11-18 | 西南化工研究设计院有限公司 | Fluidized bed propane dehydrogenation device using dehydrogenation catalyst and process thereof |
-
2011
- 2011-05-11 CN CN2011201481195U patent/CN202122945U/en not_active Expired - Lifetime
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013177723A1 (en) * | 2012-06-01 | 2013-12-05 | 中国石油天然气集团公司 | Process for producing olefin by dehydrogenation of alkane |
| CN103449948A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气集团公司 | Method for preparing olefin through dehydrogenating alkane |
| CN103449948B (en) * | 2012-06-01 | 2015-02-25 | 中国石油天然气集团公司 | Method for preparing olefin through dehydrogenating alkane |
| CN104069778A (en) * | 2013-03-27 | 2014-10-01 | 中国石油天然气集团公司 | On-line sulfuration fluidized bed reaction device for olefin production by alkane dehydrogenation and method |
| CN104069779B (en) * | 2013-03-27 | 2016-08-31 | 中国石油天然气集团公司 | The fluidized bed reaction of a kind of dehydrating alkanes alkene and method |
| CN104069778B (en) * | 2013-03-27 | 2016-08-31 | 中国石油天然气集团公司 | The fluidized bed reaction of a kind of online sulfonate hydrocarbons dehydrogenation alkene and method |
| CN111632573A (en) * | 2015-06-26 | 2020-09-08 | 陶氏环球技术有限责任公司 | Fluid solid contacting device |
| CN111632573B (en) * | 2015-06-26 | 2022-05-03 | 陶氏环球技术有限责任公司 | Fluid solid contacting device |
| CN108654526A (en) * | 2017-04-01 | 2018-10-16 | 中国石油大学(华东) | A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing |
| CN109603690B (en) * | 2019-01-08 | 2021-10-22 | 上海河图工程股份有限公司 | A reforming reactor and its application |
| CN112569872A (en) * | 2020-11-24 | 2021-03-30 | 西南化工研究设计院有限公司 | Moving bed system for preparing low-carbon olefin by dehydrogenating low-carbon alkane |
| CN115350652A (en) * | 2022-08-04 | 2022-11-18 | 西南化工研究设计院有限公司 | Fluidized bed propane dehydrogenation device using dehydrogenation catalyst and process thereof |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SHANGHAI HOTO ENGINEERING PLC Free format text: FORMER NAME: SHANGHAI HOTO PETROCHEMICAL ENGINEERING CO., LTD. |
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| CP01 | Change in the name or title of a patent holder |
Address after: 201108 Shanghai City, Minhang District Jin Road, building D, No. 392, No. 4299 Patentee after: Shanghai Hoto Engineering Inc. Address before: 201108 Shanghai City, Minhang District Jin Road, building D, No. 392, No. 4299 Patentee before: Shanghai HEC Co., Ltd. |
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| CX01 | Expiry of patent term | ||
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Granted publication date: 20120125 |